CN103755515A - Method and equipment for producing benzene and dimethyl benzene through methylbenzene dismutation - Google Patents
Method and equipment for producing benzene and dimethyl benzene through methylbenzene dismutation Download PDFInfo
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- CN103755515A CN103755515A CN201410000858.8A CN201410000858A CN103755515A CN 103755515 A CN103755515 A CN 103755515A CN 201410000858 A CN201410000858 A CN 201410000858A CN 103755515 A CN103755515 A CN 103755515A
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Abstract
The invention discloses a method and equipment for producing benzene and dimethyl benzene through methylbenzene dismutation. The equipment consists of a raw material preheater, a raw material heat exchanger, a raw material heater, a reaction rectifying tower, a reaction rectifying tower reboiler, a reaction rectifying tower top cooler, a reaction rectifying tower top reflux tank, a stripping tower, a stripping tower feed preheater, a stripping tower reboiler, a stripping tower top cooler, a dimethyl benzene product cooler, a benzene product cooler and a stripping tower top reflux tank. The method for producing benzene and dimethyl benzene through reactive rectification realizes the one-way conversion rate of 95-99wt% of the toluene disproportionation process. The method disclosed by the invention eliminates a lot of flows of toluene circulation in the toluene disproportionation process, avoids the processes of toluene warming, vaporization, cooling, condensation, re-warming and re-vaporization, and saves about 46-80% of energy consumption. The reaction rectifying tower and stripping tower used in the method replace the original reactor, stripping tower, benzene tower and toluene tower, the flow structure is simple, and the equipment investment is significantly reduced.
Description
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Technical field
The present invention relates to the production technique of benzene and dimethylbenzene, specifically, relate to a kind of toluene disproportionation and produce benzene
Method and equipment thereof with dimethylbenzene.
Background technology
China's industrial energy consumption approximately surpasses whole society's total energy consumption 70%, and the energy consumption of unit product level of many energy-intensive commercial runs is higher by 30～80% than international most advanced level.The energy-saving and emission-reduction synergy of high energy-consuming industry be society, economy and environment Sustainable development in the urgent need to.
Benzene and dimethylbenzene are important Chemical Solvents and basic organic chemical industry raw materials, are widely used in and produce industrial solvent, plastics, rubber, fiber, medicine, dyestuff, agrochemical.Utilizing toluene to produce benzene and dimethylbenzene is that the hot procedure such as to react, separated be main high energy consumption, high material-consumption process industrial.Existing toluene disproportionation produces benzene and dimethylbenzene relates to the important energy consumption equipments such as reactor, stripping tower, benzene tower and toluene tower, lack and consider that the process innovation that energy synthesis is optimized designs with the overall situation integrated, exist subject matter as follows: (1) toluene disproportionation process is subject to Equilibrium limit, and dimethylbenzene per pass conversion is low; (2) in toluene disproportionation process device, reaction product dimethylbenzene cannot shift out reaction system in time, causes side reaction to increase, and target product dimethylbenzene yield further reduces; (3) unreacted toluene, reaction product benzene and dimethylbenzene are all nearly boiling point materials, cause that flow process is complicated, separating device investment is large, energy consumption is high; (4) a large amount of unreacteds completely toluene in whole flow process, circulate, the process that have intensification repeatedly, vaporization, cooling, condensation, heats up and vaporize again, energy wastage is serious.Therefore, the energy-saving process innovation of toluene disproportionation highly energy-consuming process is very important to reducing benzene and xylene production cost, the minimizing energy and resource consumption.
Summary of the invention
The object of the invention is the deficiency existing in existing Technology, provide a kind of flow process is simple, energy consumption is little toluene disproportionation to produce method and the equipment thereof of benzene and dimethylbenzene.
The object of the invention is to be achieved by the following technical programs:
Toluene disproportionation is produced an equipment for benzene and dimethylbenzene, feed preheater, raw material interchanger, feed heater, reactive distillation column, reactive distillation column reboiler, reactive distillation tower top water cooler, reactive distillation tower top return tank, stripping tower, stripping tower feed preheater, stripping tower reboiler, stripping tower top water cooler, dimethylbenzene reactor product cooler, benzaldehyde product water cooler and stripping return tank of top of the tower, consists of;
Feed preheater outlet is connected with the import of raw material interchanger by pipeline, raw material heat exchanger exit is connected with feed heater import by pipeline, feed heater outlet is connected with reactive distillation column feed entrance by pipeline, the bottom of reactive distillation column is connected with raw material heat exchange import with reactive distillation column reboiler entrance respectively by pipeline, the outlet of reactive distillation column reboiler is connected with the entrance of reactive distillation tower bottom by pipeline, raw material heat exchanger exit is connected with dimethylbenzene reactor product cooler entrance by pipeline, the outlet of dimethylbenzene reactor product cooler goes out device connection by pipeline and dimethylbenzene product, reactive distillation top of tower is connected with feed preheater entrance by pipeline, feed preheater outlet is connected with reactive distillation tower top water cooler entrance by pipeline, reactive distillation tower top cooler outlet is connected with reactive distillation tower top return tank entrance by pipeline, reactive distillation tower top return tank gaseous phase outlet goes out device connection by pipeline and fuel gas, reactive distillation tower top return tank liquid-phase outlet is connected with stripping tower feed preheater entrance with the reflux inlet of reactive distillation top of tower respectively by pipeline, the outlet of stripping tower feed preheater is connected with stripping tower feed entrance by pipeline, by pipeline, import is connected with stripping tower feed preheater with stripping tower reboiler entrance respectively in stripping tower bottom, the outlet of stripping tower reboiler is connected with the entrance of stripping tower bottom by pipeline, the outlet of stripping tower feed preheater is connected with the entrance of benzaldehyde product water cooler by pipeline, the outlet of benzaldehyde product water cooler goes out device connection by pipeline and benzaldehyde product, stripping tower top is connected with stripping tower top water cooler entrance by pipeline, stripping tower top cooler outlet is connected with stripping return tank of top of the tower entrance by pipeline, stripping return tank of top of the tower gaseous phase outlet goes out device connection by pipeline and fuel gas, stripping return tank of top of the tower liquid-phase outlet goes out device connection with stripping tower top and light hydrocarbon product respectively by pipeline.
Utilize aforesaid device to produce the method for benzene and dimethylbenzene, comprise the steps:
(1) raw material toluene is after boosting to 1.8 ~ 3.6MPa, incoming stock preheater and the heat exchange of reactive distillation overhead gas phase, then incoming stock interchanger and the heat exchange of product dimethylbenzene, more incoming stock well heater is warming up to 240 ~ 300 ℃ of conversion zones through reactive distillation column and carries out disproportionation reaction;
(2) at the bottom of reactive distillation column, dimethylbenzene, after raw material interchanger and the heat exchange of charging toluene, then enters dimethylbenzene reactor product cooler and is cooled to 40 ~ 60 ℃ as product carrying device;
(3) reactive distillation overhead gas is after feed preheater and the heat exchange of charging toluene, after being cooled to 35 ~ 45 ℃, reactive distillation tower top water cooler enters again reactive distillation column top return tank, non-condensable gas directly goes out device to be used as fuel gas, return tank liquid phase is divided two-way: a road liquid phase is returned to reactive distillation top of tower, another road enters stripping tower feed preheater, and enters stripping tower after products benzene heat exchange;
(4) stripping tower bottom benzene is after stripping tower feed preheater and stripping tower charging heat exchange, then enters benzaldehyde product water cooler and be cooled to 40 ~ 60 ℃ as product carrying device;
(5) stripping top gaseous phase enters stripping tower top return tank after stripping tower top water cooler is cooled to 35 ~ 45 ℃, non-condensable gas directly goes out device to be used as fuel gas, return tank liquid phase is divided two-way: a road liquid phase is returned to stripping tower top, and another road goes out device as light hydrocarbon product.
In aforementioned production method, described reactive distillation tower top pressure is 1.6 ~ 3.6MPa, and tower top temperature is 220～270 ℃, and column bottom temperature is 260 ~ 320 ℃; Described stripping tower pressure on top surface is 0.5 ~ 0.9MPa, and tower top temperature is 120～150 ℃, and column bottom temperature is 160～220 ℃.
In aforementioned production method, the present invention's raw material used is that purity is toluene more than 90.0wt%, and products benzene purity is 96.0 ~ 99.6 wt%, and product dimethylbenzene purity is 95.0 ~ 99.0wt%.
Compared with prior art, the present invention has following beneficial effect:
(1) the present invention uses reactive distillation to produce the method for benzene and dimethylbenzene, by the reaction system that is continuously removed of reaction product benzene and dimethylbenzene, makes toluene disproportionation process constantly to destination party to movement, has realized the transformation efficiency of toluene disproportionation process one way 95 ~ 99 wt%;
(2) the inventive method is by the coupling of toluene disproportionation process and benzene, xylene separation process, eliminated the flow process of a large amount of toluene circulations in traditional toluene disproportionation process, the process that avoided toluene intensification, vaporization, cooling, condensation, heats up and vaporize again, energy efficient 46% ~ 80%;
(3) the present invention uses reactive distillation column and stripping tower to substitute original reactor, stripping tower, benzene tower and toluene tower, and flowage structure is simple, and facility investment significantly reduces.
Accompanying drawing explanation
Fig. 1 is the device structure schematic diagram that toluene disproportionation is produced benzene and dimethylbenzene.
Fig. 2 is the production technological process that utilizes present device.
Wherein, 1 is feed preheater, and 2 is raw material interchanger, 3 is feed heater, and 4 is reactive distillation column, and 5 is reactive distillation column reboiler, 6 is dimethylbenzene reactor product cooler, and 7 is reactive distillation tower top water cooler, and 8 is reactive distillation tower top return tank, 9 is stripping tower feed preheater, 10 is stripping tower, and 11 is stripping tower reboiler, and 12 is benzaldehyde product water cooler, 13 is stripping tower top water cooler, and 14 is stripping return tank of top of the tower.
Embodiment
As shown in Figure 1, toluene disproportionation is produced an equipment for benzene and dimethylbenzene, feed preheater 1, raw material interchanger 2, feed heater 3, reactive distillation column 4, reactive distillation column reboiler 5, reactive distillation tower top water cooler 7, reactive distillation tower top return tank 8, stripping tower 10, stripping tower feed preheater 9, stripping tower reboiler 11, stripping tower top water cooler 13, dimethylbenzene reactor product cooler 6, benzaldehyde product water cooler 12 and stripping return tank of top of the tower 14, consists of, feed preheater 1 outlet is connected with 2 imports of raw material interchanger by pipeline, 2 outlets of raw material interchanger are connected with feed heater 3 imports by pipeline, feed heater 3 outlets are connected with reactive distillation column 4 feed entrances by pipeline, by pipeline, 2 imports are connected with raw material interchanger with reactive distillation column reboiler 5 entrances respectively in the bottom of reactive distillation column 4, 5 outlets of reactive distillation column reboiler are connected with the entrance of reactive distillation column 4 bottoms by pipeline, 2 outlets of raw material interchanger are connected with dimethylbenzene reactor product cooler 6 entrances by pipeline, 6 outlets of dimethylbenzene reactor product cooler go out device connection by pipeline and dimethylbenzene product, reactive distillation column 4 tops are connected with feed preheater 1 entrance by pipeline, feed preheater 1 outlet is connected with reactive distillation tower top water cooler 7 entrances by pipeline, 7 outlets of reactive distillation tower top water cooler are connected with reactive distillation tower top return tank 8 entrances by pipeline, reactive distillation tower top return tank 8 gaseous phase outlets go out device connection by pipeline and fuel gas, reactive distillation tower top return tank 8 liquid-phase outlets are connected with stripping tower feed preheater 9 entrances with the reflux inlet at reactive distillation column 4 tops respectively by pipeline, 9 outlets of stripping tower feed preheater are connected with stripping tower 10 feed entrances by pipeline, by pipeline, 9 imports are connected with stripping tower feed preheater with stripping tower reboiler 11 entrances respectively in stripping tower 10 bottoms, 11 outlets of stripping tower reboiler are connected with the entrance of stripping tower 10 bottoms by pipeline, 9 outlets of stripping tower feed preheater are connected with the entrance of benzaldehyde product water cooler 12 by pipeline, the outlet of benzaldehyde product water cooler 12 goes out device connection by pipeline and benzaldehyde product, stripping tower 10 tops are connected with stripping tower top water cooler 13 entrances by pipeline, 13 outlets of stripping tower top water cooler are connected with stripping return tank of top of the tower 14 entrances by pipeline, stripping return tank of top of the tower 14 gaseous phase outlets go out device connection by pipeline and fuel gas, stripping return tank of top of the tower 14 liquid-phase outlets go out device connection with stripping tower top and light hydrocarbon product respectively by pipeline.
During production, will be input in technique containing toluene and the parallel feeding of a small amount of C9, catalyzer adopts solid loading type, and technique is as follows:
(1) raw material toluene is after boosting to 1.8 ~ 3.6MPa, incoming stock preheater and the heat exchange of reactive distillation overhead gas phase, then incoming stock interchanger and the heat exchange of product dimethylbenzene, more incoming stock well heater is warming up to 240 ~ 300 ℃ of conversion zones through reactive distillation column and carries out disproportionation reaction;
(2) at the bottom of reactive distillation column, dimethylbenzene, after raw material interchanger and the heat exchange of charging toluene, then enters dimethylbenzene reactor product cooler and is cooled to 40 ~ 60 ℃ as product carrying device;
(3) reactive distillation overhead gas is after feed preheater and the heat exchange of charging toluene, after being cooled to 35 ~ 45 ℃, reactive distillation tower top water cooler enters again reactive distillation column top return tank, non-condensable gas directly goes out device to be used as fuel gas, return tank liquid phase is divided two-way: a road liquid phase is returned to reactive distillation top of tower, another road enters stripping tower feed preheater, and enters stripping tower after products benzene heat exchange;
(4) stripping tower bottom benzene is after stripping tower feed preheater and stripping tower charging heat exchange, then enters benzaldehyde product water cooler and be cooled to 40 ~ 60 ℃ as product carrying device;
(5) stripping top gaseous phase enters stripping tower top return tank after stripping tower top water cooler is cooled to 35 ~ 45 ℃, non-condensable gas directly goes out device to be used as fuel gas, return tank liquid phase is divided two-way: a road liquid phase is returned to stripping tower top, and another road goes out device as light hydrocarbon product.
It is 273 ~ 284 ℃ that toluene enters reactive distillation column temperature, and pressure is 2.9 ~ 3.3MPa.Reactive distillation tower top pressure is 2.7 ~ 2.9MPa, and tower top temperature is 242～247 ℃, and column bottom temperature is 296 ~ 303 ℃; Stripping tower pressure on top surface is 0.7 ~ 0.8MPa, and tower top temperature is 138～142 ℃, and column bottom temperature is 199～207 ℃.
Use chemical-process simulation software ASPEN PLUS to carry out analog calculation to reactive distillation column, stripping tower whole process, reactive distillation column calculation result is as shown in table 1, and dimethylbenzene product purity can reach 98.5 wt%, and toluene level is 0.8 wt%; Stripping tower calculation result is as shown in table 2, benzaldehyde product purity 99.3 wt%.
Table 1 shows, by implementing this technique, almost can obtain whole p-Xylol products at the bottom of reactive distillation column tower; Table 2 shows, in stripping tower, nearly all products benzene can be separated.Meanwhile, in products benzene and dimethylbenzene, the content of raw material toluene, all lower than 1%, illustrates that toluene per pass conversion significantly improves.
Produce benzene with traditional toluene disproportionation and compare with dimethylbenzene, this technique one way can realize toluene and more than 99% transform, and has eliminated traditional unreacted separation and the circulation process of toluene completely, reduces energy consumption 62 ~ 68%.
The analog calculation of table 1 Aspen Plus reactive distillation column forms (massfraction)
The analog calculation of table 2 Aspen Plus stripping tower forms (massfraction)
Claims (3)
1. toluene disproportionation is produced an equipment for benzene and dimethylbenzene, it is characterized in that being comprised of feed preheater (1), raw material interchanger (2), feed heater (3), reactive distillation column (4), reactive distillation column reboiler (5), reactive distillation tower top water cooler (7), reactive distillation tower top return tank (8), stripping tower (10), stripping tower feed preheater (9), stripping tower reboiler (11), stripping tower top water cooler (13), dimethylbenzene reactor product cooler (6), benzaldehyde product water cooler (12) and stripping return tank of top of the tower (14);
Feed preheater (1) outlet is connected with raw material interchanger (2) import by pipeline, raw material interchanger (2) outlet is connected with feed heater (3) import by pipeline, feed heater (3) outlet is connected with reactive distillation column (4) feed entrance by pipeline, by pipeline, import is connected with raw material interchanger (2) with reactive distillation column reboiler (5) entrance respectively in the bottom of reactive distillation column (4), reactive distillation column reboiler (5) outlet is connected with the entrance of reactive distillation column (4) bottom by pipeline, raw material interchanger (2) outlet is connected with dimethylbenzene reactor product cooler (6) entrance by pipeline, dimethylbenzene reactor product cooler (6) outlet goes out device connection by pipeline and dimethylbenzene product, reactive distillation column (4) top is connected with feed preheater (1) entrance by pipeline, feed preheater (1) outlet is connected with reactive distillation tower top water cooler (7) entrance by pipeline, reactive distillation tower top water cooler (7) outlet is connected with reactive distillation tower top return tank (8) entrance by pipeline, reactive distillation tower top return tank (8) gaseous phase outlet goes out device connection by pipeline and fuel gas, reactive distillation tower top return tank (8) liquid-phase outlet is connected with stripping tower feed preheater (9) entrance with the reflux inlet at reactive distillation column (4) top respectively by pipeline, stripping tower feed preheater (9) outlet is connected with stripping tower (10) feed entrance by pipeline, by pipeline, import is connected with stripping tower feed preheater (9) with stripping tower reboiler (11) entrance respectively in stripping tower (10) bottom, stripping tower reboiler (11) outlet is connected with the entrance of stripping tower (10) bottom by pipeline, stripping tower feed preheater (9) outlet is connected with the entrance of benzaldehyde product water cooler (12) by pipeline, the outlet of benzaldehyde product water cooler (12) goes out device connection by pipeline and benzaldehyde product, stripping tower (10) top is connected with stripping tower top water cooler (13) entrance by pipeline, stripping tower top water cooler (13) outlet is connected with stripping return tank of top of the tower (14) entrance by pipeline, stripping return tank of top of the tower (14) gaseous phase outlet goes out device connection by pipeline and fuel gas, stripping return tank of top of the tower (14) liquid-phase outlet goes out device connection with stripping tower top and light hydrocarbon product respectively by pipeline.
2. the method for utilizing device fabrication benzene and dimethylbenzene described in claim 1, is characterized in that comprising the steps:
(1) raw material toluene is after boosting to 1.8 ~ 3.6MPa, incoming stock preheater and the heat exchange of reactive distillation overhead gas phase, then incoming stock interchanger and the heat exchange of product dimethylbenzene, more incoming stock well heater is warming up to 240 ~ 300 ℃ of conversion zones through reactive distillation column and carries out disproportionation reaction;
(2) at the bottom of reactive distillation column, dimethylbenzene, after raw material interchanger and the heat exchange of charging toluene, then enters dimethylbenzene reactor product cooler and is cooled to 40 ~ 60 ℃ as product carrying device;
(3) reactive distillation overhead gas is after feed preheater and the heat exchange of charging toluene, after being cooled to 35 ~ 45 ℃, reactive distillation tower top water cooler enters again reactive distillation column top return tank, non-condensable gas directly goes out device to be used as fuel gas, return tank liquid phase is divided two-way: a road liquid phase is returned to reactive distillation top of tower, another road enters stripping tower feed preheater, and enters stripping tower after products benzene heat exchange;
(4) stripping tower bottom benzene is after stripping tower feed preheater and stripping tower charging heat exchange, then enters benzaldehyde product water cooler and be cooled to 40 ~ 60 ℃ as product carrying device;
(5) stripping top gaseous phase enters stripping tower top return tank after stripping tower top water cooler is cooled to 35 ~ 45 ℃, non-condensable gas directly goes out device to be used as fuel gas, return tank liquid phase is divided two-way: a road liquid phase is returned to stripping tower top, and another road goes out device as light hydrocarbon product.
3. method as claimed in claim 2, is characterized in that, described reactive distillation tower top pressure is 1.6 ~ 3.6MPa, and tower top temperature is 220～270 ℃, and column bottom temperature is 260 ~ 320 ℃; Described stripping tower pressure on top surface is 0.5 ~ 0.9MPa, and tower top temperature is 120～150 ℃, and column bottom temperature is 160～220 ℃.
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| CN201410000858.8A CN103755515B (en) | 2014-01-02 | 2014-01-02 | A kind of toluene disproportionation produces benzene and the method for dimethylbenzene and equipment thereof |
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| CN201410000858.8A CN103755515B (en) | 2014-01-02 | 2014-01-02 | A kind of toluene disproportionation produces benzene and the method for dimethylbenzene and equipment thereof |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107213666A (en) * | 2016-03-22 | 2017-09-29 | 河南永大化工有限公司 | The separator of benzene in a kind of alkylation of toluene methanol reaction product |
| CN114100558A (en) * | 2021-11-26 | 2022-03-01 | 东营威联化学有限公司 | Equipment for producing benzene and xylene by toluene disproportionation |
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| JP2929393B2 (en) * | 1990-11-30 | 1999-08-03 | 月島機械株式会社 | Xylene production apparatus and production method |
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2014
- 2014-01-02 CN CN201410000858.8A patent/CN103755515B/en not_active Expired - Fee Related
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| JP2929393B2 (en) * | 1990-11-30 | 1999-08-03 | 月島機械株式会社 | Xylene production apparatus and production method |
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Non-Patent Citations (1)
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| 吴海波: "节能技术在歧化装置上的应用", 《石油石化节能与减排》, vol. 2, no. 3, 31 December 2013 (2013-12-31) * |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107213666A (en) * | 2016-03-22 | 2017-09-29 | 河南永大化工有限公司 | The separator of benzene in a kind of alkylation of toluene methanol reaction product |
| CN107213666B (en) * | 2016-03-22 | 2023-10-31 | 河南永大化工科技有限公司 | Separation device for benzene in toluene methanol alkylation reaction product |
| CN114100558A (en) * | 2021-11-26 | 2022-03-01 | 东营威联化学有限公司 | Equipment for producing benzene and xylene by toluene disproportionation |
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